EP0970735A1 - Verfahren und Vorrichtung zur Bearbeitung eines für expandierende Schaumbildung empfindlichen Reaktionsmediums - Google Patents

Verfahren und Vorrichtung zur Bearbeitung eines für expandierende Schaumbildung empfindlichen Reaktionsmediums Download PDF

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Publication number
EP0970735A1
EP0970735A1 EP99390010A EP99390010A EP0970735A1 EP 0970735 A1 EP0970735 A1 EP 0970735A1 EP 99390010 A EP99390010 A EP 99390010A EP 99390010 A EP99390010 A EP 99390010A EP 0970735 A1 EP0970735 A1 EP 0970735A1
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EP
European Patent Office
Prior art keywords
reaction medium
liquid
nozzle
jet
tank
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP99390010A
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English (en)
French (fr)
Inventor
Manuel Bermejo
Jean-Pierre Grasa
Jean-Marie Pernin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Biotrade SARL
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Biotrade SARL
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Publication date
Application filed by Biotrade SARL filed Critical Biotrade SARL
Publication of EP0970735A1 publication Critical patent/EP0970735A1/de
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/02—Foam dispersion or prevention
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0042—Degasification of liquids modifying the liquid flow
    • B01D19/0047—Atomizing, spraying, trickling
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/02—Means for regulation, monitoring, measurement or control, e.g. flow regulation of foam
    • C12M41/04—Means for foam enhancement

Definitions

  • the invention relates to the treatment of a reaction medium, hereinafter referred to as "foaming reaction medium", comprising at least one homogeneous or heterogeneous liquid phase (comprising several non-liquid miscible and / or at least one solid or colloidal phase such as particles in suspension), and a gaseous phase (a gas or a gaseous mixture) introduced in contact with the liquid phase, this reaction medium being susceptible, at least under certain conditions, to cause an expansive foaming resulting from the formation of gas phase bubbles in the liquid phase.
  • a reaction medium hereinafter referred to as "foaming reaction medium”
  • a reaction medium comprising at least one homogeneous or heterogeneous liquid phase (comprising several non-liquid miscible and / or at least one solid or colloidal phase such as particles in suspension), and a gaseous phase (a gas or a gaseous mixture) introduced in contact with the liquid phase, this reaction medium being susceptible, at least under certain conditions, to cause an expansive foaming resulting from the
  • Foaming reaction media pose the problem of control of expansive foaming, especially since it is frequent that these phenomena of expansive foaming appear untimely, unpredictable, and very quickly.
  • Foaming reaction media pose the problem of control of expansive foaming, especially since it is frequent that these phenomena of expansive foaming appear untimely, unpredictable, and very quickly.
  • the overflow of foam is not admissible, for many reasons (pollution, loss of materials, loss of reaction control, ).
  • FR-2,333,409 recommended separating the foam produced and throw it against the baffles of a foam breaker. As in devices seeking to break foam mechanically, this solution is expensive and is not effective enough in the presence of brutal foaming and fast.
  • FR-2,690,458 describes a process in which a prior saponification of fats, and indicates that the development of foams must be stabilized. To do this, this document recommends using a intense agitation caused by a large air flow, considering that the expansion foaming phenomenon is linked to insufficient agitation. It is nevertheless also rightly planned to incorporate an anti-foaming product into the reaction medium.
  • SU-1,414,793 describes an installation in which collects the foam formed by suction to re-inject it into the medium reactive. This solution is also limited to weak foamings expansive.
  • the invention therefore aims to overcome these drawbacks.
  • the invention is not intended to prevent the occurrence of foaming phenomena expansive, but to allow, when such expansive foaming occurs, prevent overflow of foam.
  • the invention aims to avoid foam overflows without requiring the complete interruption of treatment.
  • the invention aims to allow, in the presence of expansive foaming, continue the treatment of a foaming reaction medium, avoiding all foam overflow.
  • the invention also aims to obtain this result in a way extremely simple and economical.
  • the invention also aims to provide a process and installation for treating a foaming reaction medium -in particular advantageously applicable for fermentation or for aerobic biological degradation of organic lipid compositions such as greasy waste of animal or vegetable origin in an aqueous medium in the presence of a bacterial biomass (activated sludge) -, which are particularly simple, efficient, and inexpensive to invest and operate.
  • a foaming reaction medium in particular advantageously applicable for fermentation or for aerobic biological degradation of organic lipid compositions such as greasy waste of animal or vegetable origin in an aqueous medium in the presence of a bacterial biomass (activated sludge) -, which are particularly simple, efficient, and inexpensive to invest and operate.
  • the invention aims to propose a method and a treatment plant in which the introduction of gases into the medium reaction and mixing of the reaction medium is obtained so particularly simple - especially without the need for submerged devices (baffles, chimneys, mixers ...) -, and efficient - notably without leaving dead volume (untreated) of reaction medium.
  • the inventors have found that when the foam arrives at the height of each nozzle emitting a jet of plunging liquid (s), the absence of any other source of introduction of gas into the reaction medium, the foam height stabilizes and never exceeds the height of the nozzle.
  • the function of the plunging liquid (s) is not only to introduce gas in the reaction medium, but also to limit by construction the height of foam formed resulting from this introduction of gas.
  • the liquid (s) forming this jet (s) can (can) be formed from at least one starting liquid composition continuously feeding the reaction medium, in the case where the invention is applied to the treatment of a foaming reaction medium requiring such continuous feeding.
  • a circulating medium comprising at least a liquid phase which is discharged under pressure by at least one nozzle forming a jet of liquid (s) immersed in the reaction medium.
  • said circulating medium is the reaction medium as extracted from the bottom of the tank.
  • each nozzle is fixed fixed, permanently, at a height HB lower than that HR of the walls sides of the tank and higher than that HM of the surface of the liquid phase of the reaction medium.
  • a height HB lower than that HR of the walls sides of the tank and higher than that HM of the surface of the liquid phase of the reaction medium.
  • a method according to the invention is also characterized in that a tank having at least side walls is used substantially cylindrical in revolution, and a bottom at least substantially frustoconical and in that it directs at least one jet of liquid (s) plunging with a non-zero inclination relative to a diametrical plane of the tank passing through the crossing point above the side walls of the pipe supplying the nozzle, this plunging liquid (s) jet also serving as means for stirring the reaction medium.
  • the inclination of the jet of liquid (s) plunging relative to the diametral plane is between 15 ° and 75 °, -in particular is of the order of 30 °.
  • the jet (s) of plunging liquid (s) has the function of introducing the gas into the medium reactive; to limit the formation of foam to a predetermined height and therefore to prevent any overflow of foam; and ensure the mixing of the medium reactive.
  • the inclination of the jet of liquid (s) plunging from the vertical is between 10 ° and 30 ° -in particular of the order of 20 ° -.
  • the invention extends to an installation for implementing a method according to the invention.
  • the bottom of the tank is at least substantially frustoconical in shape.
  • the extraction pipe is connected to a lower end of the bottom frustoconical of the tank.
  • the angle at the top from the bottom of the tank is between 30 ° and 60 ° - in particular of the order of 45 ° -.
  • a installation according to the invention is characterized in that it comprises a tank having at least substantially cylindrical side walls of revolution, and a at least substantially frustoconical bottom, and in that at least one nozzle is oriented with a non-zero inclination relative to the diametrical plane of the tank passing through the crossing point above the side walls of the pipe feeding the nozzle, the jet of plunging liquid (s) coming from this nozzle acting means for stirring the reaction medium.
  • the inclination of the nozzle relative to the diametral plane is understood between 15 ° and 75 ° - in particular is of the order of 30 ° -.
  • At least a nozzle is oriented with a non-zero inclination relative to the vertical.
  • the inclination of the nozzle relative to the vertical is between 10 ° and 30 ° -in particular of the order of 20 °.
  • at least one nozzle is arranged at a distance from the surface of the liquid phase (s) of the reaction medium between one third and two thirds of the width of the tank at this level area.
  • the invention also relates to a method and an installation characterized in combination by all or some of the characteristics mentioned above or below.
  • the invention also extends to the application of a method and of an installation according to the invention for carrying out a degradation treatment aerobic biological of organic lipid compositions, such as waste fatty of animal or vegetable origin, in an aqueous medium in the presence of a bacterial biomass (activated sludge) placed in the tank.
  • the reaction medium then comprises an aqueous lipid medium containing lipid compositions to be treated, a nitrogen and phosphorus amendment, bacterial biomass, and air and / or oxygen as a gas introduced into the liquid phase by the jet (s) of plunging liquid (s).
  • the installation shown in the figures includes a tank 1 intended to contain a reaction medium 2 comprising at least one phase liquid.
  • the tank 1 has a bottom bottom 3 which is at least substantially shaped frustoconical, the angle at the top of the bottom 3 being between 30 ° and 60 ° -in particular of the order of 45 ° as shown in Figure 1-.
  • the tank 1 includes also, above and from the bottom 3, side walls 4 which, in the example shown, are vertical cylindrical walls of revolution around of the axis of symmetry of the frustoconical bottom 3.
  • the bottom 3 defines a lower reference level 5, for example the lower end of the frustoconical bottom 3. From this level lower reference, heights can be defined. Thus, the side walls 4 extend over a height HR from the lower reference level 5.
  • An extraction pipe 6 is connected to the end bottom 7 of the bottom 3 via an extraction valve 8.
  • This extraction line 6 is extended, on one side by a purge line 9 by via a purge valve 10.
  • the extraction pipe 6 is connected to a pump 11, for example of the centrifugal type, via a valve 12.
  • the centrifugal pump 11 is driven by a motor 13 and delivers the medium extracted by the extraction pipe 6 in a discharge pipe 14 which extends upwards along the side walls 4 of the tank, and of which the free end is provided with a nozzle 15 disposed fixed inside the tank 1 to deliver a jet of liquid (s) 16 plunging into the liquid phase of the medium reaction 2.
  • a flow meter 17 is interposed on the discharge pipe 14.
  • the reaction medium to be treated is introduced into tank 1 by a supply line 18 opening above the middle level reaction 2 contained in tank 1.
  • the tank 1 is provided with means making it possible to regulate the level of reaction medium 2 in tank 1 at a fixed HM height predetermined lower than the height HR of the side walls 4.
  • a orifice 20 formed in the lower part of the side walls 4 opens into a level control line 19 which extends from the opening 20 upwards to form a bend 21 at the nominal height HM of the reaction medium 2.
  • This pipe 19 acts as a siphon, so that the middle level reaction 2 cannot exceed the height HM thus defined.
  • the middle reaction possibly evacuated via this level control line 19 can be reintroduced via the supply line 18 if this reaction medium is not fully treated, or is discharged as a treated medium if the treatment is finished, a new quantity of medium to be treated being supplied by the supply line 18.
  • the tank 1 is also provided with a foam detector 22 which may consist of an exposed electrical conductor wire so as to form a electrical contact when the foam reaches this conductor electric.
  • This foam detector 22 is placed in the tank 1 at a height which is at least substantially the same as that HB of the nozzle 15 at the end free from discharge line 14 or slightly greater than this height HB.
  • the foam detector 22 is connected to an automaton 23 which manages the supply of the reaction medium via the supply line 18.
  • the height HB of the nozzle 15 delivering the jet of liquid (s) 16 plunging is less than the height HR of the walls but greater than the height HM of the reaction medium 2 contained in the tank 1.
  • the nozzle 15 is placed above the surface 24 of the liquid phase of the medium reaction 2, so that the jet of liquid (s) 16 plunging into this phase liquid has a free length 25 capable of entraining the gas disposed above of the liquid phase of the reaction medium 2 in the tank 1 around the nozzle 15.
  • This gas is, in the example shown, atmospheric air, the tank 1 being open at its top. None prevents, however, from providing that the tank 1 is hermetically sealed with a lid, a suitable gas separate from air atmospheric can be introduced into the tank 1 at its upper part above of the liquid phase of the reaction medium 2.
  • This gas can for example be oxygen.
  • the reaction medium 2 is a foaming reaction medium, that is, a foam 26 normally forms above the surface 24 of the liquid phase of the reaction medium 2, during the reaction.
  • a foam 26 normally forms above the surface 24 of the liquid phase of the reaction medium 2, during the reaction.
  • the foam 26 extends over a small height above the surface 24, no phenomenon of expansive foaming being observed.
  • This foam 26 results from the introduction of gas into the reaction medium 2 by the jet liquid 16 which also acts as stirring of the reaction medium 2.
  • the liquid jet 16 thus arranged makes it possible to limit the height of the foam 26 expansive possibly formed above the surface 24 of the liquid phase of reaction medium 2 at height HB, so that any overflow of foam is avoided.
  • Figures 3 and 4 show in more detail the shape and the orientation of the nozzle 15.
  • the discharge line 14 passes over the edge free upper 27 of the side walls 4 at a passage point 28, and is connected to the interior 1 of the tank 1 at the nozzle 15. It is thus possible to define a diametral plane 29 vertical of the tank 1 passing through this crossing point 28.
  • the nozzle 15 extends in a vertical plane 30 which is inclined at an angle ⁇ with respect to the diametrical plane 29, so that the jet of liquid 16 immersed in the reaction medium 2 and which comes from the nozzle 15 acts as means of stirring the reaction medium 2.
  • the tank 1 shown is free from any other stirring or mixing means, the only jet of liquid 16 acting, with the frustoconical shape of the bottom 3, of means of stirring the reaction medium 2.
  • the inclination ⁇ , the frustoconical shape of the bottom 3 and the circulation of the reaction medium 2 extracted via the pipe 6 and discharged through the nozzle 15, ensure extremely mixing effective reaction medium 2, as well as an introduction of the gas into this medium reactional 2.
  • the inclination ⁇ can vary within a range of values relatively large between 15 ° and 75 °. In the example shown, the inclination ⁇ is of the order of 30 ° and this value has been found to be particularly effective and beneficial.
  • the value of the inclination ⁇ can be optimized by a function of the nature, in particular of the viscosity, of the reaction medium. the same goes for the inclination of the frustoconical bottom 3.
  • the angle ⁇ can be oriented to correspond to a entrainment of the reaction medium 2 by the jet of liquid plunging 16 into the direction of the natural vortex, or in the opposite direction to the natural vortex.
  • the nozzle 15 is also oriented with a inclination ⁇ relative to the vertical and this inclination a is advantageously between 10 ° and 30 ° -in particular of the order of 20 ° ( Figure 3) -.
  • the inclinations a and ⁇ are determined so that optimize the introduction of the gas into the reaction medium 2 and the movement imparted to the liquid phase of the reaction medium 2 by the liquid jet 16 which arrives at the surface 24 of the liquid phase of the reaction medium 2 at an impact point 31 located at least substantially in the middle of the radius of the tank 1.
  • the nozzle 15 is arranged at a height of the surface 24 of the liquid phase of the reaction medium 2, which is adapted in particular according to the desired ventilation performance and the geometry tank 1.
  • the shape of the nozzle 15, its end section, the section of the discharge line 14 which supplies it and the discharge pressure delivered by the pump 11 are also characteristics which influence the characteristics of the liquid jet 16 and its effectiveness.
  • the calculation of these different dimensional parameters is well known to those skilled in the art (cf. for example "Gas entrainement by planging liquid jets” Chemical Engeniery Science, Vol. 48, No 21, 1993).
  • the nozzle 15 is oriented to drive the reaction medium 2 rotating around the vertical axis of the tank 1. This rotation can be performed either in the direction of the natural vortex, or in the direction contrary to the natural vortex.
  • This rotation associated with the frustoconical shape of the bottom 3 ensures that all of the reaction medium 2 is stirred, without no dead volume inside the tank 1.
  • the heaviest particles contained in reaction medium 2 for example the bacterial biomass under flock form in the case of the treatment of lipid compositions with a bacterial biomass, are dragged towards the axis and towards the lower end 7 bottom extraction 3.
  • the tank 1 thus has a hydrodynamic structure of infinitely mixed type favorable to the implementation of numerous reactions chemical or biochemical - especially in the context of biological treatment greasy residue.
  • the tank 1 is free from any wall internal vertical (baffle, chimney, ...), any other means of mixing than liquid jet 16, and any other means for introducing gas than this liquid jet 16.
  • the installation according to the invention is therefore particularly simple, economical to investment, use, and maintenance.
  • the fact that the nozzle 15 is arranged at a height HB less than the height HR of the side walls 4 allows to limit the height of the expansive foam 26 possibly formed above the reaction medium 2.
  • the inventors believe that an explanation possible of this result would be that when this expansive foam arrives at the height of the end of the nozzle 15, the liquid jet 16 is entirely surrounded by foam and no longer or almost no more additional gas capable of forming foam inside the liquid phase of the reaction medium 2. It is noted in any case in practice that the foam 26 remains confined to a height corresponding at least substantially to the height HB of the nozzle 15.
  • the height of the expansive foam formed does not generally correspond exactly to the height HB of the nozzle 15, and exceeds this height HB by a value which depends on the nature of the foam. However, it can be seen that there is always a certain height of foam at from which the expansive foaming stops, the foam never exceeding this height above the nozzle 15.
  • aqueous lipid medium to be treated is introduced via the pipe 18.
  • the pump 11 can be kept running in such a way to continue the reaction. If you want to stop the reaction, you can also otherwise stop the pump. Simultaneously, the treated medium is removed by the level control line 19. The pump 11 is then again put into operation operation, if it had been previously stopped, and we see that the previously formed expansive foams are broken and return to the nominal foam height as shown in figure 1.
  • the tank 1 has a diameter of 800 mm, a frustoconical bottom with an angle at the top of 45 ° extending over a height of 370 mm.
  • the surface 24 of the liquid defined by the level regulation pipe 19 is 1280 mm from the lower reference level 5, and the side walls have a height RH of 1980 mm.
  • the nozzle 15 is at 1,630 mm from level 5, the angle a is equal to 20 ° and the angle ⁇ is equal to 30 °.
  • the working volume thus defined in tank 1 is 500 l.
  • the pump 11 provides a flow rate of 3.5 m 3 / h and the exit speed of the liquid jet 16 is 8 m / s.
  • aqueous lipid medium was treated in this installation, the reaction medium comprising 35 g / l of suspended matter (bacterial biomass).
  • the automaton 23 is programmed to supply 10 l of aqueous lipid medium every 8 h, unless detection of expansive foaming by detector 22.
EP99390010A 1998-06-11 1999-05-21 Verfahren und Vorrichtung zur Bearbeitung eines für expandierende Schaumbildung empfindlichen Reaktionsmediums Withdrawn EP0970735A1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9807365 1998-06-11
FR9807365A FR2779660B1 (fr) 1998-06-11 1998-06-11 Procede et installation pour le traitement d'un milieu reactionnel susceptible de provoquer un moussage expansif

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EP0970735A1 true EP0970735A1 (de) 2000-01-12

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EP99390010A Withdrawn EP0970735A1 (de) 1998-06-11 1999-05-21 Verfahren und Vorrichtung zur Bearbeitung eines für expandierende Schaumbildung empfindlichen Reaktionsmediums

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FR (1) FR2779660B1 (de)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2831831B1 (fr) * 2001-11-06 2004-01-02 Christophe Montigny Procede pour la maitrise du foisonnement de la mousse produite par le melangeage d'un liquide moussant et d'un gaz, sur les procedes a chute de liquide
FR2836481A1 (fr) * 2002-02-22 2003-08-29 Reithem Dispositif pour la culture sur site de micro-organismes, tels que des bacteries
CN102765774A (zh) * 2011-05-04 2012-11-07 哈尔滨工业大学 分散硅氧烷脂质吸附剂去除水中持久性有机污染物的方法
CN109797810B (zh) * 2019-01-17 2024-05-07 广东省水利水电科学研究院 一种应用于高水头供水构筑物的弯管分流消泡装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2633126A1 (de) * 1975-07-26 1977-02-17 Agency Ind Science Techn Verfahren und vorrichtung zur beseitigung von auf einer fluessigkeitsoberflaeche auftretendem schaum
FR2334409A1 (fr) * 1975-12-10 1977-07-08 Sulzer Ag Dispositif de traitement de liquides
US4952509A (en) * 1988-04-14 1990-08-28 Phillips Petroleum Company Fermentation broth degassification

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2633126A1 (de) * 1975-07-26 1977-02-17 Agency Ind Science Techn Verfahren und vorrichtung zur beseitigung von auf einer fluessigkeitsoberflaeche auftretendem schaum
FR2334409A1 (fr) * 1975-12-10 1977-07-08 Sulzer Ag Dispositif de traitement de liquides
US4952509A (en) * 1988-04-14 1990-08-28 Phillips Petroleum Company Fermentation broth degassification

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
CHEMICAL ABSTRACTS, vol. 76, no. 18, 1 May 1972, Columbus, Ohio, US; abstract no. 101622d, RIHA MILAN: "scrubbing separator for foamy mxtures in gases" page 117; column r; XP002095096 *

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Publication number Publication date
FR2779660A1 (fr) 1999-12-17
FR2779660B1 (fr) 2000-08-18

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